JP7449413B2 - Fluidized bed reactor, apparatus and method for producing light olefins from oxygenated compounds - Google Patents

Description

The present application belongs to the field of chemical industrial catalysis and relates to a fluidized bed reactor, apparatus and method for producing light olefins from oxygenated compounds.

The technology for producing alkenes from methanol (MTO) mainly includes the DMTO (manufacturing of alkenes from methanol) technology of the Dalian Institute of Chemical Physics, Chinese Academy of Sciences, and the MTO technology of the American UOP company. In 2010, a plant for producing alkenes from Shenhua Baotou methanol using DMTO technology was built and became operational. This is the world's first industrial application of MTO technology, and by the end of 2019, 14 sets of DMTO industrial equipment were already in operation, with a total light olefin production capacity of about 8 million tons/year.

In recent years, DMTO technology has further developed, and new generation DMTO catalysts with better performance have gradually begun to be applied in industrial applications, creating higher profits for DMTO factories. New generation DMTO catalysts have higher methanol processing capacity and light olefin selectivity. It is difficult for conventional DMTO industrial equipment to take full advantage of the advantages of new generation DMTO catalysts, so we are developing DMTO equipment and manufacturing methods that can meet the demands for new generation DMTO catalysts with high methanol processing capacity and high light olefin selectivity. Research and development is necessary.

According to one aspect of the present application, a fluidized bed reactor is provided, which is capable of on-line reforming a DMTO catalyst by coke-controlled reaction, and the reforming described herein is , to control the coke content, coke content distribution and coke species in the DMTO catalyst, thereby controlling the DMTO catalyst performance and improving the selectivity of light olefins.

The light olefins mentioned herein are ethylene and propene.

The research conducted by the present inventors has revealed that the main factors that influence the activity of the DMTO catalyst and the selectivity of light olefins are the coke content, coke content distribution, and coke type in the catalyst. For the same average coke content of the catalyst, a narrow coke content distribution results in high selectivity for light olefins and high activity. The coke species in the catalyst include polymethyl aromatic hydrocarbons and polymethyl cyclic alkanes, where polymethylbenzene and polymethylnaphthalene can promote the production of ethylene. Therefore, controlling the coke content, coke content distribution, and coke species in the catalyst is the key to controlling the activity of the DMTO catalyst and improving the selectivity of light olefins.

According to a first aspect of the present application, a fluidized bed reactor is provided. The fluidized bed reactor includes a reactor housing, a reaction zone, a coke control zone, and a transport tube;
The reactor housing includes a lower housing and an upper housing, the lower housing surrounds a reaction area, and the transport tube is provided above the reaction area and communicates with the reaction area, an upper housing is provided around the outer periphery of the transport pipe, the upper housing and the transport pipe surrounding a cavity containing a coke control region;
A gas outlet is provided at the upper part of the transport pipe,
the reaction zone includes a reaction feed inlet and a coke control catalyst inlet;
The coke control region includes a catalyst inlet, a coke control catalyst outlet, a coke control gas outlet, and a coke control feed inlet;
the coke control region is an annular chamber;
In the coke control area, n baffle plates are provided, the n baffle plates divide the coke control area into n sub-coke control areas, and the n sub-coke control areas are: including a first sub-coke control region, a second sub-coke control region to an n-th sub-coke control region,
Each of the n-1 baffle plates is provided with at least one catalyst flow hole so that the catalyst flows along an annular shape within the coke control region, where n is an integer;
The catalyst inlet is provided in a first sub-coke control region, the coke control catalyst outlet is provided in an n-th sub-coke control region, and the coke control gas outlet is provided between two adjacent baffle plates. It will be done.

If the coke control zone includes only one zone, the residence time distribution of the catalyst entering said coke control zone will approximate the residence time distribution of a fully mixed kettle reactor, and under such conditions, the coke control obtained will be The uniformity of the coke content on the catalyst particles is relatively poor, that is, the coke content of some catalyst particles is very low, and the coke content of some catalyst particles is very high, so that the average activity of the catalyst is relatively poor. , resulting in a relatively low average selectivity. In the present application, a coke control zone is installed, a baffle plate is installed along the radial direction in the coke control zone, and the coke control zone is divided into several coke control zone sub-zones, whereby the retention of the catalyst entering the coke control zone is achieved. By controlling the time distribution, the coke content distribution in the coke control catalyst is narrow, the average activity is relatively high, and the average selectivity is relatively high. At the same time, adopting the zoned control method is also advantageous in controlling the coke species and coke content on the coke control catalyst.

Optionally, the first baffle plate does not have the catalyst flow holes, and the second to nth baffle plates each have the catalyst flow holes.

Optionally, the diameter of the coke control zone herein is smaller than the diameter of the reaction zone.

Preferably, the diameter of the coke control zone increases from bottom to top.

Optionally, a first sub-coke control region divided by the first baffle plate and the second baffle plate is provided with a coke control region catalyst inlet;
A coke control catalyst transport pipe communicating with the reaction region is provided in the n-th sub-coke control region divided by the first baffle plate and the n-th baffle plate, and the coke control catalyst transport pipe is connected to the coke control catalyst transport pipe. One end of the coke control catalyst outlet is located at the coke control catalyst outlet, and the other end is located at the reaction zone.

Preferably, the coke control catalyst transport pipe is further provided with a coke control catalyst sliding valve for controlling circulation of the catalyst.

A coke control area distributor is provided below the sub-coke control area,
The coke control gas outlet is connected to the transport pipe via a coke control zone gas transport pipe.

In this application, a coke control area is installed, baffle plates arranged concentrically and sequentially are installed in the coke control area, and the baffle plates have flow holes to divide the coke control area into several sub-coke control areas. , the catalyst forms an annular flow within the coke control zone, thereby controlling the residence time of the catalyst entering the coke control zone and the mode of coke control. That is, when controlling in each sub-region, the content of catalyst in the control space is relatively uniform so that the distribution of coke content on the catalyst is narrow, and the coke species and coke content on the catalyst are also controlled. become. The coke content of some catalyst particles is low and the coke content of some catalyst particles is very high, which avoids causing a wide distribution of coke content of the catalyst.

Optionally, 2≦n≦10.

Specifically, the number of catalyst flow holes opened in the baffle plate may be one or more, and the present application is not strictly limited. When a plurality of catalyst flow holes are provided, the relative positions of the catalyst flow holes are not strictly limited in this application either; for example, the plurality of catalyst flow holes may be arranged in parallel or randomly arranged. You may.

In the present application, the shape of the coke control catalyst transport pipe is not strictly limited, as long as it ensures that the coke control catalyst transport pipe can deliver the coke control catalyst to the reaction zone, for example, an elongated shape with a bent structure. It may be a pipe or, of course, may be of any other suitable shape.

Preferably, a coke control area distributor is provided below each sub-coke control area. In this way, it can be realized that the whole coke control material enters the coke control region uniformly, and the coke control material between each sub-region avoids the occurrence of uneven phenomenon, and the catalytic coke content distribution is narrow. We can better realize what we want to become.

Optionally, the cross-section of the coke control region is annular, and the cross-section of the sub-coke control region is sector-shaped.

Optionally, the coke control gas outlet is connected to the transport pipe via a coke control zone gas transport pipe.

Optionally, the bottom of the sub-coke control zone is provided with a coke control zone distributor;
The coke control feed inlet is in communication with the coke control zone distributor, or the coke control feed inlet is located below the coke control zone distributor.

Preferably, the bottom of each sub-coke control zone is provided with a coke control zone distributor.

Optionally, the reaction raw material inlet is provided with a reaction zone distributor installed at the bottom of the reaction zone.

Specifically, the reaction zone distributor is used to pass reaction raw materials.

Specifically, in the present application, the reaction raw material is a raw material containing an oxygen-containing compound.

Optionally, the fluidized bed reactor further includes a spent agent region, the spent agent region is provided above the coke control region and fitted around the outer circumference of the transport pipe, and the spent agent region is disposed above the coke control region and fitted around the outer circumference of the transport pipe, A partition plate is provided between the agent region and the coke control region,
A spent agent area distributor is provided at the bottom of the spent agent area.

Optionally, the spent agent area further includes a fluidized bed reactor heat remover.

Optionally, the fluidized bed reactor further includes a solid-gas separation region provided above the spent agent region and fitted around the outer periphery of the transport pipe,
The solid-gas separation region is provided with a solid-gas separator,
The spent agent region is in communication with the solid-gas separation region.

Optionally, the solid-gas separator includes a first solid-gas separator and a second solid-gas separator,
an inlet of the first solid-gas separator is in communication with the transport pipe, a catalyst outlet of the first solid-gas separator is provided in the spent agent region,
A catalyst outlet of the second solid-gas separator is also provided in the spent agent region.

Optionally, the fluidized bed reactor further includes a product gas transport pipe and a gas collection chamber, and the product gas transport pipe and the gas collection chamber are provided in the upper part of the reactor housing, and the product gas a transport pipe is provided at the top of the reactor housing, the product gas transport pipe is connected to the top of the gas collection chamber,
A gas outlet of the second solid-gas separator is connected to the gas collection chamber, and a gas outlet of the first solid-gas separator is connected to the gas collection chamber.

Optionally, the fluidized bed reactor further includes a spent agent circulation pipe provided outside the reactor housing.

The inlet of the spent agent circulation tube is connected to the spent agent region, and the outlet of the spent agent circulation tube is connected to the bottom of the reaction zone.

Optionally, the spent agent circulation pipe is further provided with a spent agent circulation slide valve for controlling the circulation of the spent catalyst.

According to a second aspect of the present application, there is further provided a method for producing light olefins from oxygenated compounds. The process is carried out using at least one of the fluidized bed reactors mentioned above.

Optionally, the method comprises:
passing a coke control feedstock and a catalyst from a regenerator to a coke control region and reacting to produce a coke control catalyst and a coke control product gas;
and forming an annular flow of the catalyst through catalyst flow holes on the baffle plate.

Optionally, the method comprises:
A coke control feed is passed from a coke control zone distributor into a coke control zone, a catalyst is passed through a catalyst inlet into a coke control zone, and the coke control feed and the catalyst are catalytically reacted in the coke control zone, and coke producing a control catalyst and a coke control product gas, the coke control catalyst entering the reaction zone via the coke control catalyst outlet, and the coke control product gas entering the transport pipe via the coke control gas outlet; 1) and
(2) feeding a feed containing oxygenates from a reactant feed inlet to a reaction zone and contacting a coke control catalyst to obtain stream A containing light olefins.

Optionally, the coke control feedstock includes C ₁ -C ₆ hydrocarbon-based compounds.

Preferably, the hydrocarbon compound is at least one selected from C ₁ to C ₆ alkanes and C ₁ to C ₆ alkenes.

Optionally, the coke control raw material further includes at least one of hydrogen gas, an alcohol compound, and water;
The mass content of the total content of the alcohol compound and water in the coke control raw material is 10 wt% or more and 50 wt% or less.

Preferably, the alcohol compound is at least one selected from methanol and ethanol.

Optionally, the coke control feedstock includes hydrogen gas 0-20 wt%, methane 0-50 wt%, ethane 0-50 wt%, ethylene 0-20 wt%, propane 0-50 wt%, propene 0-20 wt%, butane 0-50 wt%. 90wt%, butene 0-90wt%, pentane 0-90wt%, pentene 0-90wt%, hexane 0-90wt%, hexene 0-90wt%, methanol 0-50wt%, ethanol 0-50wt%, water 0-50wt% including;
The hydrocarbon compound is not zero.

Optionally, the oxygen-containing compound is at least one selected from methanol and dimethyl ether.

Optionally, the catalyst comprises a SAPO molecular sieve,
The coke content in the coke control catalyst is 4 to 9 wt,
The interquartile deviation of the coke content distribution in the coke control catalyst is less than 1 wt%.

Specifically, in this application, by installing a coke control region and selecting a coke control process, the coke content in the coke control catalyst is 4 to 9 wt%, and since the catalyst is particulate, the coke content of the catalyst is Although the coke content is the average value of the coke content of each catalyst particle, the coke content of each catalyst particle is not actually the same. In this application, the interquartile deviation of the coke content distribution in the coke control catalyst may be controlled within a range of less than 1 wt% so that the coke content distribution across the catalyst is narrow, thereby increasing the activity of the catalyst. and improve selectivity for light olefins.

Optionally, the coke species in the coke control catalyst include polymethylbenzene and polymethylnaphthalene;
The content of the total mass of the polymethylbenzene and polymethylnaphthalene in the total mass of coke is ≧70 wt%,
The content of the mass of coke species with a molecular weight >184 in the total mass of coke is ≦25 wt%;
Here, the total mass of coke is the total mass of coke species.

In the present application, the type of coke species and the content of coke species are also very important and are also one of the control objectives of the present application. In this application, the installation of coke control and the selection of coke control process parameters achieve the effect that the content of polymethylbenzene and polymethylnaphthalene in the total coke mass is ≧70 wt%, the activity of the catalyst, and the selection of light olefins. Improved sex.

Optionally, the process operating conditions of the coke control region include gas apparent linear velocity of 0.1~0.5 m/s, reaction temperature of 300~700°C, reaction pressure of 100~500 kPa, and bed density of 400~0.5 m/s. 800 kg/ ^m3 ,
The process operating conditions in the reaction zone are: gas apparent linear velocity of 0.5 to 7.0 m/s, reaction temperature of 350 to 550°C, reaction pressure of 100 to 500 kPa, and bed density of 100 to 500 kg/ ^m3 . be.

Optionally, after said step (2),
forming a mixed stream B in a transport pipe of a stream A containing light olefins and a coke control product gas exiting from a coke control gas outlet, the flow B passing through the transport pipe to a first solid-gas separator; It further comprises a step (3) of entering and solid-gas separation and then dividing into a gas phase stream C, which is a gas containing light olefins, and a solid phase stream D, which is a spent catalyst.

Optionally, the coke content in the spent catalyst is between 9 and 13 wt%.

Optionally, after said step (3),
the gas phase stream C enters the gas collection chamber, the solid phase stream D enters the spent agent region, and passes the spent agent zone fluidizing gas into the spent agent zone from the spent agent zone fluidizing gas inlet; The method further includes the step (4) of contacting the spent catalyst and forming stream E of the spent agent zone fluidizing gas and its supported spent catalyst.

Optionally, the spent agent region fluidizing gas includes at least one of nitrogen gas and water vapor.

Optionally, after said step (4),
Stream E enters the second solid-gas separator, and after being separated into solid-gas, it is divided into a gas-phase flow F, which is a spent agent zone fluidizing gas, and a solid-phase flow G, which is a spent catalyst. Stream F enters the gas collection chamber, solid phase flow G enters the spent agent region, gas phase stream C and gas phase stream F mix in the gas collection chamber to form a product gas, and the product gas The method further includes a step (5) of entering the downstream process through a gas transport pipe.

Optionally, after said step (5),
The method further comprises a step (6) of returning the spent catalyst in the spent agent zone to the bottom of the reaction zone of the fluidized bed reactor via a spent agent circulation pipe.

Optionally, the process operating conditions of the spent agent region include gas apparent linear velocity of 0.1-1.0 m/s, reaction temperature of 350-550°C, reaction pressure of 100-500 kPa, and bed density of 200 m/s. ~800 kg/ ^m3 .

According to a third aspect of the present application, an apparatus is further provided. The apparatus includes a fluidized bed reactor and a fluidized bed regenerator, the fluidized bed reactor communicating with the fluidized bed regenerator,
The fluidized bed reactor is at least one selected from the fluidized bed reactors described above.

Optionally, the fluidized bed regenerator includes a regenerator housing;
the regenerator housing is provided with a spent catalyst inlet;
the spent catalyst inlet is in communication with a spent agent region of the fluidized bed reactor;
Preferably, the spent catalyst inlet is in communication with the spent agent region of the fluidized bed reactor via a first stripper.

More preferably, the spent agent region of the fluidized bed reactor and the first stripper are communicated via a spent inclined tube.

Optionally, the first stripper and the spent catalyst inlet communicate via a spent agent transport tube.

Preferably, the spent agent transport pipe is provided with a spent slide valve for controlling circulation of the catalyst.

Specifically, the apparatus for producing light olefins from oxygen-containing compounds provided by the present application is equipped with a fluidized bed regenerator, and utilizes the fluidized bed regenerator to regenerate a used catalyst. A catalyst is passed through a coke control zone to perform coke control, and after coke control is passed to a reaction zone to perform a catalytic reaction. Catalyst can be brought online and coke control can be done online, improving production efficiency.

Optionally, a bottom end of the regenerator housing is in communication with the coke control region;
Preferably, a bottom end of the regenerator housing is in communication with the coke control region via a second stripper;
Preferably, a regenerator heat remover is provided within said second stripper.

Optionally, the regenerator housing is further provided with a regenerator distributor;
One end of the second stripper extends into the regenerator housing.

Optionally, the second stripper and the regenerated catalyst inlet communicate through a regenerant transport pipe.

Preferably, the regenerant transport pipe is provided with a regeneration slide valve.

Optionally, the fluidized bed regenerator further includes a regenerator solid-gas separator, a regenerator gas collection chamber, and a flue gas transport pipe,
The regenerator solid-gas separator is provided in the regenerator housing, the regenerator gas collection chamber and the flue gas transport pipe are provided in the upper part of the regenerator housing, and the flue gas transport pipe is arranged in the regenerator housing. provided at the top of the regenerator housing, the flue gas transport pipe being connected to the top of the regenerator gas collection chamber;
A gas outlet of the regenerator solid-gas separator is connected to the regenerator gas collection chamber, and a regenerated catalyst outlet of the regenerator solid-gas separator is provided at a lower part of the regenerator housing.

According to a fourth aspect of the present application, there is further provided a method of producing light olefins from oxygenated compounds. The method is performed using at least one of the devices described above.

Optionally, the method includes spending catalyst in a spent agent zone entering the fluidized bed regenerator and, after being regenerated in the fluidized bed regenerator, entering the coke control zone.

Optionally, the method comprises:
step (a) of said spent catalyst entering the middle part of a fluidized bed regenerator after being stripped through a first stripper;
Regeneration gas is passed through the regeneration gas inlet to the bottom of the fluidized bed regenerator, contacting the regeneration gas with the spent catalyst and causing a chemical reaction to produce stream H containing flue gas and regenerated catalyst; enters the regenerator solid-gas separator, after solid-gas separation, it is divided into flue gas and regenerated catalyst, the flue gas enters the regenerator gas collection chamber, and then passes through the flue gas transport pipe to the downstream exhaust gas. After entering the smoke treatment system, the regenerated catalyst returns to the bottom of the fluidized bed regenerator, and the regenerated catalyst in the fluidized bed regenerator enters the second stripper, where it is stripped and heat removed before coke control of the fluidized bed reactor. (b) entering the region.

Preferably, the coke content in the regenerated catalyst is ≦3 wt%.

Optionally, the regeneration gas is at least one selected from oxygen gas, nitrogen gas, water vapor, and air.

Preferably, the regeneration gas includes 0 to 100 wt% air, 0 to 50 wt% oxygen gas, 0 to 50 wt% nitrogen gas, and 0 to 50 wt% water vapor.

Optionally, the process operating conditions of the fluidized bed regenerator include gas apparent linear velocity of 0.5-2.0 m/s, regeneration temperature of 600-750°C, regeneration pressure of 100-500 kPa, and bed density of 150 m/s. ~700 kg/ ^m3 .

Optionally, the coke content in the regenerated catalyst is ≦3 wt%.

The method for producing the light olefin includes:
The spent catalyst in the spent agent region is passed through a fluidized bed regenerator for regeneration treatment to produce a regenerated catalyst, and the regenerated catalyst is passed into a coke control region of the fluidized bed reactor to produce a coke control feedstock. further comprising the step of contacting and reacting with.

Specifically, the fluidized bed reactor according to the present application is divided into a reaction zone, a coke control zone, a spent agent zone, and a solid-gas separation zone from bottom to top. The method includes contacting a coke control feedstock and a catalyst in a coke control region of a fluidized bed reactor to produce a coke control product gas and a coke control catalyst, the coke control catalyst entering a reaction region of the fluidized bed reactor; In the reaction zone, the feedstock containing oxygenates and the coke control catalyst are contacted to produce a product gas containing light olefins and spent catalyst; b) contacting the catalyst to produce flue gas and regenerated catalyst, and said regenerated catalyst flowing into the coke control zone.

The C ₁ to C ₆ hydrocarbon compound in the present application is a hydrocarbon compound having 1 to 6 carbon atoms.

Beneficial effects of the present application include the following.
(1) The catalyst in this application is distributed from the upstream sub-region downstream through catalyst flow holes in the baffle plate in the coke control region so that (i) catalyst storage in the coke control region can be automatically adjusted; By controlling the average residence time of the catalyst in the coke control zone, the coke content in the catalyst can be controlled. (ii) The coke content distribution is narrow by controlling the residence time distribution of the catalyst by adopting a structure of n sub-coke control regions whose residence time distribution approximates n series fully mixed kettle reactors. I got a catalyst.
(2) By controlling the conversion and generation of coke species in the catalyst, the present application can, on the one hand, convert inactive polymer coke species remaining in the catalyst into low molecular coke species, and on the other hand, coke control. The raw material can enter into the catalyst to produce highly active low molecular coke species, and the low molecular coke species are mainly polymethylbenzene and polymethylnaphthalene, which can improve the selectivity of ethylene. .
(3) The method of online reforming of DMTO catalyst by coke control reaction in this application is a coke control catalyst with high coke content, narrow coke content distribution, and where the main components of coke species are polymethylbenzene and polymethylnaphthalene. and convert a catalyst with relatively low light olefin selectivity into a coke control catalyst with high light olefin selectivity.
(4) The catalyst of the present application may be used directly in the process of producing light olefins from oxygenated compounds without going through a coke control process, and if the catalyst does not go through a coke control process, the light The selectivity for olefins is 80-83 wt%, and the catalyst of the present application is used in a process for producing light olefins from oxygenated compounds after undergoing coke control process treatment, and the selectivity for light olefins in the resulting product gas is was 93 to 96 wt%.
(5) In the method of the present application, the apparent linear velocity of the gas in the reaction zone of the fluidized bed reactor is high, a relatively high methanol flux can be obtained, and the methanol throughput per unit volume of the equipment can be improved. The mass hourly space velocity can reach 5-20 h ^-1 , and the spent agent zone absorbs heat, lowers the temperature of the spent catalyst, transports the spent catalyst to the reaction zone at a lower temperature, and increases the bed density in the reaction zone. , which is used to control the bed temperature in the reaction zone, and when the apparent linear velocity of the gas was 0.5-7.0 m/s, the corresponding bed density was 500-100 kg/m ³ .
(6) The fluidized bed reactor of the present application adopts a structure in which the first solid-gas separator of the fluidized bed reactor is directly connected to the transport pipe, and the gas containing light olefins in stream B is removed from the spent catalyst. A rapid separation was achieved, avoiding further reaction of light olefins under the action of spent catalyst to produce alkanes by-products with larger molecular weights.

1 is a schematic diagram of an apparatus for producing light olefins (DMTO) from oxygen-containing compounds according to one embodiment of the present application. 1 is a cross-sectional schematic diagram of a coke control region of a fluidized bed reactor according to one embodiment of the present application; FIG.

The present application will be described in detail below with reference to Examples, but the present application is not limited to these Examples.

Unless otherwise specified, all raw materials and catalysts used in the Examples of this application are purchased as commercially available products.

The SAPO molecular sieve used in the examples of this application was purchased from Zhongke Huahua (Dalian) Co., Ltd.

In order to improve the performance of DMTO catalyst, this application provides a method for on-line reforming of DMTO catalyst by coke-controlled reaction, which method comprises:
(1) sending the catalyst to a coke control zone;
(2) sending the coke control feedstock to the coke control region;
A step in which the coke control feedstock and the catalyst are brought into contact and reacted in a coke control region, and the coke control feedstock is coked on the catalyst, the catalyst after being coked is called a coke control catalyst, and the coke control feedstock is coked on the catalyst. The coke content is 4 to 9 wt%, the coke types include polymethylbenzene and polymethylnaphthalene, and the content of polymethylbenzene and polymethylnaphthalene in the total coke mass is ≧70 wt% and the content of the mass of coke species having a molecular weight of >184 in the total mass of coke is ≦25 wt%;
(4) sending a coke control catalyst to the reaction zone.

The catalyst is a DMTO catalyst with a coke content of ≦3 wt%, and the active component of the DMTO catalyst is a SAPO molecular sieve.

The reaction temperature of the coke control reaction is 300-700°C.

The present application further provides a method for producing light olefins from an oxygen-containing compound, including a method for on-line reforming the above-mentioned DMTO catalyst by a coke-controlled reaction, and an apparatus using the method. The apparatus includes a fluidized bed reactor 1 and a fluidized bed regenerator 2.

Apparatus for producing light olefins from oxygenates, said apparatus comprising a fluidized bed reactor 1, said fluidized bed reactor 1 comprising, from bottom to top, a reaction zone, a coke control zone, The fluidized bed reactor 1 is divided into a spent agent area and a solid-gas separation area, and includes a reactor housing 1-1, a reaction area distributor 1-2, a transport pipe 1-3, and a coke control area distributor 1-4. , baffle plate 1-5, coke control region gas transport pipe 1-6, spent agent region distributor 1-7, fluidized bed reactor heat remover 1-8, first solid-gas separator 1-9, first 2 solid-gas separator 1-10, gas collection chamber 1-11, produced gas transport pipe 1-12, coke control catalyst transport pipe 1-13, coke control catalyst sliding valve 1-14, spent agent circulation pipe 1- 15, including a used agent circulation slide valve 1-16, a used inclined pipe 1-17, a first stripper 1-18, a used agent circulation slide valve 1-19 and a used agent transport pipe 1-20;
The reaction zone distributor 1-2 is located at the bottom of the reaction zone of the fluidized bed reactor 1, and the transport pipe 1-3 is located at the center of the fluidized bed reactor 1, and its bottom end is located at the bottom of the reaction zone of the fluidized bed reactor 1. connected to the apex,
The coke control area is located above the reaction area, and n baffle plates 1-5 are provided in the coke control area, and the baffle plates 1-5 control the coke control area into n sub-coke control areas. n is an integer satisfying 2≦n≦10, and a coke control region distributor 1-4 is independently provided at the bottom of each sub-coke control region, and the coke control region is divided into sub-regions. The cross section is annular, the cross section of the sub-coke control region is fan-shaped, the first to nth sub-coke control regions are sequentially arranged concentrically, and the baffle plate 1-5 includes catalyst flow holes. , the baffle plate 1-5 between the first sub-coke control region and the n-th sub-coke control region does not include catalyst flow holes, and the outlet of the regenerant transport pipe 2-9 is connected to the fluidized bed reactor 1. The inlet of the coke control catalyst transport pipe 1-13 is connected to the n-th sub coke control region, and the coke control catalyst transport pipe 1-13 has a coke control catalyst A slide valve 1-14 is provided, the outlet of the coke control catalyst transport pipe 1-13 is connected to the lower part of the reaction zone, and a coke control region gas transport pipe 1-6 is provided in the upper part of the sub-coke control region. , the inlet of the coke control region gas transport pipe 1-6 is located at the upper part of the sub-coke control region, the outlet of the coke control region gas transport pipe 1-6 is connected to the transport pipe 1-3,
The spent agent area distributor 1-7 is located at the bottom of the spent agent area, and the fluidized bed reactor heat remover 1-8 is located in the spent agent area;
The first solid-gas separator 1-9, the second solid-gas separator 1-10 and the gas collection chamber 1-11 are located in the solid-gas separation area of the fluidized bed reactor 1. The inlet of the separator 1-9 is connected to the upper part of the transport pipe 1-3, and the gas outlet of the first solid-gas separator 1-9 is connected to the gas collection chamber 1-11, and the gas outlet of the first solid-gas separator 1-9 is connected to the gas collection chamber 1-11. The catalyst outlet of the separator 1-9 is located in the spent agent region, and the inlet of the second solid-gas separator 1-10 is located in the solid-gas separation region of the fluidized bed reactor 1, The gas outlet of the gas separator 1-10 is connected to the gas collection chamber 1-11, the catalyst outlet of the second solid-gas separator 1-10 is located in the spent agent area, and the product gas transport pipe 1-10 is connected to the gas collection chamber 1-11. 12 is connected to the top of the gas collection chamber 1-11,
The inlet of the spent agent circulation pipe 1-15 is connected to the spent agent region, and the outlet of the spent agent circulation pipe 1-15 is connected to the bottom of the reaction region and is connected to the spent agent circulation pipe 1-15. is provided with a used agent circulation slide valve 1-16,
The inlet of the used inclined tube 1-17 is connected to the spent agent area, the outlet of the used inclined tube 1-17 is connected to the upper part of the first stripper 1-18, and the outlet of the used inclined tube 1-17 is connected to the upper part of the first stripper 1-18. 18 is located outside the reactor housing 1-1, the inlet of the used slide valve 1-19 is connected to the bottom of the first stripper 1-18 via a conduit, and the used slide valve 1-19 is connected to the bottom of the first stripper 1-18. The outlet of 19 is connected to the inlet of the used agent transport pipe 1-20 via a pipeline, and the outlet of the used agent transport pipe 1-20 is connected to the middle part of the fluidized bed regenerator 2.

In a preferred embodiment, the first solid-gas separator 1-9 employs one or more sets of solid-gas cyclone separators, each set of solid-gas cyclone separators having one first stage. solid air cyclone separator and one second stage solid air cyclone separator.

In a preferred embodiment, the second solid-gas separator 1-10 employs one or more sets of solid-gas cyclone separators, each set of solid-gas cyclone separators having one first stage. solid air cyclone separator and one second stage solid air cyclone separator.

In a preferred embodiment, the second solid-gas separator 1-10 is a single-stage line whose inlet is located in the solid-gas separation area and whose outlet is connected to the gas collection chamber 1-11.

An apparatus for producing light olefins from oxygen-containing compounds, the apparatus including a fluidized bed regenerator 2, the fluidized bed regenerator 2 comprising a regenerator housing 2-1, a regenerator distributor 2-2. , regenerator solid-gas separator 2-3, regenerator gas collection chamber 2-4, flue gas transport pipe 2-5, second stripper 2-6, regenerator heat remover 2-7, regeneration slide valve 2- 8 and a regenerant transport pipe 2-9,
The regenerator distributor 2-2 is located at the bottom of the fluidized bed regenerator 2, and the regenerator solid-gas separator 2-3 is located at the top of the fluidized bed regenerator 2. -3 is located at the upper part of the fluidized bed regenerator 2, and the gas outlet of the regenerator solid-gas separator 2-3 is connected to the regenerator gas collection chamber 2-4, and the regenerator solid-gas separator 2-3 is connected to the regenerator gas collection chamber 2-4. The regenerated catalyst outlet of -3 is located at the bottom of the fluidized bed regenerator 2, the regenerator gas collection chamber 2-4 is located at the top of the fluidized bed regenerator 2, and the flue gas transport pipe 2-5 is located at the bottom of the fluidized bed regenerator 2. connected to the top of the gas collection chamber 2-4,
The second stripper 2-6 is located outside the regenerator housing 2-1, and the inlet pipe of the second stripper 2-6 passes through the regenerator housing 2-1 to the regenerator distributor 2. -2, the regenerator heat remover 2-7 is located in the second stripper 2-6, and the inlet of the regenerator slide valve 2-8 is connected to the second stripper through a conduit. 2-6, the outlet of the regenerating slide valve 2-8 is connected to the inlet of the regenerant transport pipe 2-9 via a pipe, and the outlet of the regenerant transport pipe 2-9 is connected to the bottom of the regenerant transport pipe 2-6. It is connected to the first sub-coke control zone in reactor 1.

In a preferred embodiment, the regenerator solid-gas separators 2-3 employ one or more sets of solid-gas cyclone separators, each set of solid-gas cyclone separators having one first stage. It includes a solid air cyclone separator and one second stage solid air cyclone separator.

According to another aspect of the present application, there is further provided a method for producing light olefins from oxygen-containing compounds using the apparatus described in any one of the above items. The method includes the following steps.
Step (1), passing the coke control feedstock from the coke control zone distributor 1-4 into the coke control zone of the fluidized bed reactor 1, and passing the catalyst through the regenerant transport pipe 2-9 to the coke control zone of the fluidized bed reactor 1; the coke control feedstock contacts the catalyst in the coke control zone to cause a chemical reaction to occur and produce a coke control catalyst and a coke control product gas, the coke control catalyst being in contact with the catalyst in the baffle plates 1-5. The coke sequentially passes through the 1-n sub-coke control area through the hole, and enters the reaction area of the fluidized bed reactor 1 via the coke control catalyst transport pipe 1-13 and the coke control catalyst sliding valve 1-14. The controlled product gas enters the transport pipe 1-3 via the coke control zone gas transport pipe 1-6, passing the feedstock containing oxygenates from the reaction zone distributor 1-2 to the reaction zone of the fluidized bed reactor 1. Stream A and coke control product gas are mixed in transport pipe 1-3 to form stream B, and are contacted with a coke control catalyst to produce stream A containing light olefins and spent catalyst; B enters the first solid-gas separator 1-9 through a transport pipe 1-3, and after being separated into solid-gas, it is separated into a gas-phase flow C, which is a gas containing light olefins, and a solid phase, which is a spent catalyst. Stream D, gas phase stream C enters the gas collection chamber 1-11, solid phase stream D enters the spent agent zone and sends the spent agent zone fluidizing gas to the spent agent zone distributor 1-7. from the spent agent zone and into contact with the spent catalyst, the spent agent zone fluidizing gas and its supported small amount of spent catalyst form stream E, which passes through the second solid-gas separator. 1-10, and after solid-gas separation, the gas phase flow F is divided into a gas phase flow F, which is a spent agent region fluidizing gas, and a solid phase flow G, which is a spent catalyst. -11, the solid phase stream G enters the spent agent region, the gas phase stream C and the gas phase stream F mix in the gas collection chamber 1-11 to form a product gas; It enters the downstream process via the transport pipe 1-12, and some of the spent catalyst in the spent agent area is transferred to the fluidized bed reactor via the spent agent circulation pipe 1-15 and the spent agent circulation slide valve 1-16. Returning to the bottom of the reaction zone 1, the used catalyst in other parts enters the first stripper 1-18 through the used inclined pipe 1-17, and after being stripped, the used catalyst is It enters the middle part of the fluidized bed regenerator 2 via the slide valve 1-19 and the spent agent transport pipe 1-20.
Step (2), passing the regeneration gas from the regenerator distributor 2-2 to the bottom of the fluidized bed regenerator 2, and in the fluidized bed regenerator 2, the regeneration gas is brought into contact with the spent catalyst to generate a chemical reaction. , some coke in the spent catalyst is combusted and removed to produce stream H containing flue gas and regenerated catalyst, stream H enters the regenerator solid-gas separator 2-3 and is subjected to solid-gas separation. After that, the flue gas is separated into the flue gas and the regenerated catalyst, and the flue gas enters the regenerator gas collection chamber 2-4, and then enters the downstream flue gas treatment system through the flue gas transport pipe 2-5, where the regenerated catalyst is Returning to the bottom of the fluidized bed regenerator 2, the regenerated catalyst in the fluidized bed regenerator 2 enters the second stripper 2-6, where it is stripped and heat removed, and then connected to the regeneration slide valve 2-8 and the regenerant transport pipe. 2-9 into the coke control zone of the fluidized bed reactor 1.

In a preferred embodiment, the components of the coke control feedstock include 0-20 wt% hydrogen gas, 0-50 wt% methane, 0-50 wt% ethane, 0-20 wt% ethylene, 0-50 wt% propane, 0-20 wt% propene. %, butane 0-90 wt%, butene 0-90 wt%, pentane 0-90 wt%, pentene 0-90 wt%, hexane 0-90 wt%, hexene 0-90 wt%, methanol 0-50 wt%, ethanol 0-50 wt%. The water content is 0 to 50 wt%.

In one preferred embodiment, the oxygenate in the above method is one of methanol or dimethyl ether or a mixture of methanol and dimethyl ether.

In one preferred embodiment, the spent agent zone fluidizing gas in the above method is one of nitrogen gas and water vapor or a mixture of nitrogen gas and water vapor.

In a preferred embodiment, the regeneration gas in the above method is 0-100 wt% air, 0-50 wt% oxygen gas, 0-50 wt% nitrogen gas, and 0-50 wt% water vapor.

In one preferred embodiment, the active component of the catalyst is a SAPO molecular sieve.

In one preferred embodiment, the coke content in the catalyst is ≦3 wt%.

In one preferred embodiment, the coke content in the coke control catalyst is between 4 and 9 wt%, the interquartile deviation of the coke content distribution in the coke control catalyst is less than 1 wt%, and the coke type includes polyester. The mass of coke species containing methylbenzene and polymethylnaphthalene, the content of polymethylbenzene and polymethylnaphthalene in the total mass of coke is ≧70 wt%, and the molecular weight is >184 in the total mass of coke. The content is ≦25 wt%.

In one preferred embodiment, the spent catalyst has a coke content of 9 to 13 wt%, and more preferably, the spent catalyst has a coke content of 10 to 12 wt%.

In a preferred embodiment, the process operating conditions of the coke control zone of the fluidized bed reactor 1 (1) include: an apparent linear velocity of gas of 0.1 to 0.5 m/s, a reaction temperature of 300 to 700°C; The reaction pressure is 100 to 500 kPa, and the bed density is 400 to 800 kg/m ³ .

In a preferred embodiment, the process operating conditions of the reaction zone of the fluidized bed reactor 1 (1) include: an apparent linear velocity of gas of 0.5 to 7.0 m/s, a reaction temperature of 350 to 550°C; The pressure is 100 to 500 kPa and the bed density is 100 to 500 kg/m ³ .

In a preferred embodiment, the process operating conditions in the spent agent region of the fluidized bed reactor 1 (1) include an apparent linear velocity of gas of 0.1 to 1.0 m/s and a reaction temperature of 350 to 550°C. , the reaction pressure is 100 to 500 kPa, and the bed density is 200 to 800 kg/m ³ .

In a preferred embodiment, the process operating conditions of the fluidized bed regenerator 2 (2) are: gas apparent linear velocity of 0.5 to 2.0 m/s, regeneration temperature of 600 to 750°C, and regeneration pressure of 100 m/s. -500kPa, bed density 150-700kg/ ^m3 .

In the above method of the present application, the components of the generated gas are 38 to 58 wt% ethylene, 35 to 57 wt% propene, C ₄ to C ₆ hydrocarbons ≦4 wt%, and ≦4 wt% of other components, and the other components are: Methane, ethane, propane, hydrogen gas, CO and _CO2, etc., and the total selectivity in the product gases of ethylene and propene is 93-96 wt%.

In this application, regarding the description of the production unit, the mass of dimethyl ether in the oxygen-containing compound is calculated by converting it into the methanol mass based on the same carbon atom mass, and the unit of the production unit is ton methanol/ton light olefin.

In the above method of the present application, the production unit is 2.50 to 2.58 tons methanol/ton light olefin.

In order to further explain the present application and facilitate understanding of the technical solution of the present application, typical and non-limiting examples of the present application are as follows.

Example 1
This embodiment uses the apparatus shown in FIGS. 1 and 2, and the coke control zone in the fluidized bed reactor includes two baffle plates, that is, n=2, and the coke control zone , two coke control region sub-regions are included, and the second solid-gas separator employs a plurality of sets of solid-gas cyclone separators, each set of solid-gas cyclone separators having one first-stage solid-gas cyclone separator. It included a pneumatic cyclone separator and one second stage solid pneumatic cyclone separator.

In this embodiment, the coke control feedstock is a mixture of 6 wt% butane, 81 wt% butene, 2 wt% methanol, and 11 wt% water, the oxygenated compound is methanol, and the spent agent zone fluidizing gas is nitrogen. The regeneration gas is air, the active component in the catalyst is SAPO-34 molecular sieve, the coke content in the catalyst is about 1 wt%, and the coke content in the coke control catalyst is about 4 wt%. Here, the content of the mass of polymethylbenzene and polymethylnaphthalene in the total coke mass is about 83 wt%, and the content of the mass of coke species with a molecular weight >184 in the total coke mass is: The interquartile deviation of the coke content distribution in the coke control catalyst was about 0.9 wt%, and the coke content in the spent catalyst was about 9 wt%. The process operating conditions in the coke control zone of the fluidized bed reactor are: gas apparent linear velocity of about 0.3 m/s, reaction temperature of about 500 °C, reaction pressure of about 100 kPa, and bed density of about 600 kg/ ^m3 . Ta. The process operating conditions in the reaction zone of the fluidized bed reactor were: gas apparent linear velocity of about 7.0 m/s, reaction temperature of about 550 °C, reaction pressure of about 100 kPa, and bed density of about 100 kg/ ^m3 . . The process operating conditions in the spent agent region of the fluidized bed reactor are: gas apparent linear velocity of about 1.0 m/s, reaction temperature of about 550°C, reaction pressure of about 100 kPa, and bed density of about 200 kg/ ^m3 . there were. The process operating conditions for the fluidized bed regenerator were: gas apparent linear velocity of about 0.5 m/s, regeneration temperature of about 700° C., regeneration pressure of about 100 kPa, and bed density of about 700 kg/m ³ .

In this embodiment, the mass hourly space velocity of the oxygenates in the fluidized bed reactor was approximately 20 h ⁻¹ . The components of the generated gas are 58 wt% ethylene, 35 wt% propene, 3 wt% C ₄ - C ₆ hydrocarbons, and 4 wt % other components, and the other components are methane, ethane, propane, hydrogen gas, CO and CO. ₂ etc. The production unit was 2.58 tons methanol/ton light olefin.

Example 2
This embodiment uses the apparatus shown in FIGS. 1 and 2, and the coke control area in the fluidized bed reactor includes ten baffle plates, that is, n=10, and the coke control area includes , ten coke control region sub-regions are included, and the second solid-gas separator employs a plurality of sets of solid-gas cyclone separators, each set of solid-gas cyclone separators having one first-stage solid-gas cyclone separator. It included a pneumatic cyclone separator and one second stage solid pneumatic cyclone separator.

In this embodiment, the coke control raw materials are 22 wt% methane, 24 wt% ethane, 3 wt% ethylene, 28 wt% propane, 4 wt% propene, a mixture of 7 wt% hydrogen gas and 12 wt% water, and the oxygen-containing compound is methanol. The spent agent zone fluidizing gas is water vapor, the regeneration gas is 50 wt% air and 50 wt% water vapor, and the active component in the catalyst is SAPO-34 molecular sieve. The coke content in the catalyst is about 3 wt%, and the coke content in the coke control catalyst is about 9 wt%, where the content in the total coke mass of polymethylbenzene and polymethylnaphthalene is is about 71 wt%, the content of the mass of coke species with molecular weight >184 in the total coke mass is about 23 wt%, and the quartile deviation of the coke content distribution in the coke control catalyst is about 0. .2 wt%, and the coke content in the spent catalyst was about 13 wt%. The process operating conditions in the coke control zone of the fluidized bed reactor are: gas apparent linear velocity of about 0.1 m/s, reaction temperature of about 300 °C, reaction pressure of about 500 kPa, and bed density of about 800 kg/ ^m3 . Ta. The process operating conditions in the reaction zone of the fluidized bed reactor were: gas apparent linear velocity of about 0.5 m/s, reaction temperature of about 350 °C, reaction pressure of about 500 kPa, and bed density of about 500 kg/ ^m3 . . The process operating conditions in the spent agent region of the fluidized bed reactor are: gas apparent linear velocity of about 0.1 m/s, reaction temperature of about 350°C, reaction pressure of about 500 kPa, and bed density of about 800 kg/ ^m3 . there were. The process operating conditions for the fluidized bed regenerator were: gas apparent linear velocity of about 2.0 m/s, regeneration temperature of about 600° C., regeneration pressure of about 500 kPa, and bed density of about 150 kg/m ³ .

In this embodiment, the mass hourly space velocity of the oxygenates in the fluidized bed reactor was approximately 5 h ⁻¹ . The components of the generated gas are 38 wt% ethylene, 57 wt% propene, 4 wt% C ₄ - C ₆ hydrocarbons, and 1 wt % other components.The other components are methane, ethane, propane, hydrogen gas, CO and CO. ₂ etc. The production unit was 2.53 tons methanol/ton light olefin.

Example 3
This embodiment uses the apparatus shown in FIGS. 1 and 2, and the coke control area in the fluidized bed reactor includes four baffle plates, that is, n=4, and the coke control area includes , four coke control region sub-regions were included, and the second solid-gas separator was a single-stage conduit with an inlet located in the solid-gas separation region and an outlet connected to the fluidized bed reactor gas collection chamber. .

In this embodiment, the coke control raw materials include 1 wt% propane, 1 wt% propene, 3 wt% butane, 51 wt% butene, 3 wt% pentane, 22 wt% pentene, 1 wt% hexane, 7 wt% hexene, 2 wt% methanol, and 9 wt% water. The oxygenated compound is dimethyl ether, the spent agent region fluidizing gas is 5 wt% nitrogen gas and 95 wt% water vapor, the regeneration gas is 50 wt% air and 50 wt% oxygen gas, and the catalyst The active ingredient in the catalyst is SAPO-34 molecular sieve, the coke content in the catalyst is about 2 wt%, and the coke content in the coke control catalyst is about 6 wt%, where polymethylbenzene and polymethylnaphthalene The content in the total coke mass of the mass of coke species with molecular weight >184 is about 80 wt%, the content of the mass of coke species with molecular weight >184 in the total coke mass is about 11 wt%, and the coke content in the coke control catalyst The interquartile deviation of the distribution was about 0.6 wt% and the coke content in the spent catalyst was about 11 wt%. The process operating conditions in the coke control zone of the fluidized bed reactor are: gas apparent linear velocity of about 0.4 m/s, reaction temperature of about 700 °C, reaction pressure of about 300 kPa, and bed density of about 500 kg/ ^m3 . Ta. The process operating conditions in the reaction zone of the fluidized bed reactor were: gas apparent linear velocity of about 3.0 m/s, reaction temperature of about 450 °C, reaction pressure of about 300 kPa, and bed density of about 230 kg/ ^m3 . . The process operating conditions in the spent agent region of the fluidized bed reactor are: gas apparent linear velocity of about 0.2 m/s, reaction temperature of about 450°C, reaction pressure of about 300 kPa, and bed density of about 600 kg/ ^m3 . there were. The process operating conditions for the fluidized bed regenerator were: gas apparent linear velocity of about 1.0 m/s, regeneration temperature of about 750° C., regeneration pressure of about 300 kPa, and bed density of about 360 kg/m ³ .

In this embodiment, the mass hourly space velocity of the oxygenates in the fluidized bed reactor was approximately 9 h ⁻¹ . The components of the generated gas are 48 wt% ethylene, 48 wt% propene, 2 wt% C ₄ - C ₆ hydrocarbons, and 2 wt % other components.The other components are methane, ethane, propane, hydrogen gas, CO and CO. ₂ etc. The production unit was 2.50 tons methanol/ton light olefin.

Example 4
This embodiment uses the apparatus shown in FIGS. 1 and 2, and the coke control area in the fluidized bed reactor includes six baffle plates, that is, n=6, and the coke control area includes , six coke control region sub-regions are included, and the second solid-gas separator employs a plurality of sets of solid-gas cyclone separators, each set of solid-gas cyclone separators having one first-stage solid-gas cyclone separator. It included a pneumatic cyclone separator and one second stage solid pneumatic cyclone separator.

In this embodiment, the coke control feedstock is a mixture of 5 wt% butane, 72 wt% butene, 8 wt% methanol, and 15 wt% water, the oxygenated compound is methanol, and the spent agent zone fluidizing gas is nitrogen. 73 wt% gas and 27 wt% water vapor, the regeneration gas is 50 wt% air and 50 wt% nitrogen gas, the active component in the catalyst is SAPO-34 molecular sieve, and the coke content in the catalyst is about 2 wt%. , the coke content in the coke control catalyst is about 6 wt%, where the content of the mass of polymethylbenzene and polymethylnaphthalene in the total coke mass is about 77 wt%, and the molecular weight is >184. The content of the mass of coke species in the total mass of coke is about 16 wt%, the interquartile deviation of the coke content distribution in the coke control catalyst is about 0.3 wt%, and the coke content in the spent catalyst is , about 12 wt%. The process operating conditions in the coke control zone of the fluidized bed reactor are: gas apparent linear velocity of about 0.5 m/s, reaction temperature of about 600 °C, reaction pressure of about 200 kPa, and bed density of about 400 kg/ ^m3 . Ta. The process operating conditions in the reaction zone of the fluidized bed reactor were: gas apparent linear velocity of about 4.0 m/s, reaction temperature of about 500 °C, reaction pressure of about 200 kPa, and bed density of about 160 kg/ ^m3 . . The process operating conditions in the spent agent zone of the fluidized bed reactor are: gas apparent linear velocity of about 0.5 m/s, reaction temperature of about 500°C, reaction pressure of about 200 kPa, and bed density of about 300 kg/ ^m3 . there were. The process operating conditions for the fluidized bed regenerator were: gas apparent linear velocity of about 1.5 m/s, regeneration temperature of about 680° C., regeneration pressure of about 200 kPa, and bed density of about 280 kg/m ³ .

In this embodiment, the mass hourly space velocity of the oxygenates in the fluidized bed reactor was approximately 13 h ⁻¹ . The components of the generated gas are 53 wt% ethylene, 42 wt% propene, 4 wt% C ₄ - C ₆ hydrocarbons, and 1 wt % other components.The other components are methane, ethane, propane, hydrogen gas, CO and CO. ₂ etc. The production unit was 2.52 tons methanol/ton light olefin.

Comparison This comparative example differs from Example 4 in that a coke control reaction online reforming DMTO catalyst is not used and the raw material introduced into the coke control region is nitrogen gas. Since nitrogen gas is an inert gas, it does not change the properties of the regenerated catalyst in the coke control zone, ie, the catalyst entering the reaction zone is a regenerated catalyst.

In this embodiment, the components of the generated gas are 44 wt% ethylene, 38 wt% propene, 10 wt% C ₄ to C ₆ hydrocarbons, and 8 wt% other components, and the other components are methane, ethane, propane, and hydrogen. gases, such as CO and _CO2 . The production unit was 2.92 tons methanol/ton light olefin.

This comparative example showed that online reforming of the DMTO catalyst by coke control reaction can significantly improve the performance of the catalyst and reduce the production unit consumption.

The above are only some embodiments of the present application, and do not limit the present application in any way. Although the present application has been disclosed above with preferred embodiments, it is not intended to limit the present application, and those skilled in the art For example, without departing from the scope of the technical proposal of the present application, any slight changes or improvements made based on the technical content disclosed above correspond to equivalent embodiments and all fall within the scope of the technical proposal. .

1 fluidized bed reactor, 1-1 reactor housing, 1-2 reaction zone distributor,
1-3 transport pipe, 1-4 coke control area distributor, 1-5 baffle plate,
1-6 Coke control area gas transport pipe, 1-7 Spent agent area distributor,
1-8 fluidized bed reactor heat remover, 1-9 first solid-gas separator,
1-10 second solid-gas separator, 1-11 gas collection chamber, 1-12 produced gas transport pipe,
1-13 Coke control catalyst transport pipe, 1-14 Coke control catalyst sliding valve,
1-15 used agent circulation pipe, 1-16 used agent circulation slide valve, 1-17 used inclined pipe,
1-18 first stripper, 1-19 used sliding valve, 1-20 used transport pipe,
2 fluidized bed regenerator, 2-1 regenerator housing, 2-2 regenerator distributor,
2-3 regenerator solid-gas separator, 2-4 regenerator gas collection chamber,
2-5 flue gas transport pipe, 2-6 second stripper, 2-7 regenerator heat remover,
2-8 regeneration slide valve, 2-9 regenerant transport pipe.

Claims (10)

A fluidized bed reactor comprising a reactor housing, a reaction zone, a coke control zone, and a transport tube, the reactor comprising:
The reactor housing includes a lower housing and an upper housing, the lower housing surrounds a reaction area, and the transport tube is provided above the reaction area and communicates with the reaction area, an upper housing is provided around the outer periphery of the transport pipe, the upper housing and the transport pipe surrounding a cavity containing a coke control region;
A gas outlet is provided at the upper part of the transport pipe,
the reaction zone includes a reaction feed inlet and a coke control catalyst inlet;
The coke control region includes a catalyst inlet, a coke control catalyst outlet, a coke control gas outlet, and a coke control feed inlet;
the coke control region is an annular chamber;
In the coke control area, n baffle plates are provided, the n baffle plates divide the coke control area into n sub-coke control areas, and the n sub-coke control areas are: including a first sub-coke control region, a second sub-coke control region to an n-th sub-coke control region,
Each of the n-1 baffle plates is provided with at least one catalyst flow hole so that the catalyst flows along an annular shape within the coke control region, where n is an integer;
The catalyst inlet is provided in a first sub-coke control region, the coke control catalyst outlet is provided in an n-th sub-coke control region, and the coke control gas outlet is provided between two adjacent baffle plates. A fluidized bed reactor characterized by: 2≦n≦10 ,
The cross-section of the coke control region is annular, and the cross-section of the sub-coke control region is fan-shaped;
The coke control gas outlet is connected to the transport pipe via a coke control region gas transport pipe.
A coke control area distributor is provided at the bottom of the sub-coke control area,
the coke control feed inlet is in communication with the coke control zone distributor, or the coke control feed inlet is located below the coke control zone distributor;
The fluidized bed reactor according to claim 1 , wherein the reaction raw material inlet is provided with a reaction zone distributor installed at the bottom of the reaction zone . The fluidized bed reactor further includes a spent agent region, the spent agent region is provided above the coke control region and fitted around the outer circumference of the transport pipe, and is connected to the spent agent region and the spent agent region. A partition plate is provided between the coke control area and the coke control area.
a used agent area distributor is provided at the bottom of the used agent area ;
The spent agent area further includes a fluidized bed reactor heat remover;
The fluidized bed reactor further includes a solid-gas separation region provided above the spent agent region and fitted around the outer periphery of the transport pipe, and the solid-gas separation region includes a solid-gas separator. provided, the spent agent region is in communication with the solid-gas separation region,
The solid-gas separator includes a first solid-gas separator and a second solid-gas separator, an inlet of the first solid-gas separator communicates with the transport pipe, and an inlet of the first solid-gas separator communicates with the transport pipe. a catalyst outlet of the solid-gas separator is provided in the spent agent region;
a catalyst outlet of the second solid-gas separator is also provided in the spent agent region;
The fluidized bed reactor further includes a product gas transport pipe and a gas collection chamber, the product gas transport pipe and the gas collection chamber are provided in the upper part of the reactor housing, and the product gas transport pipe is configured to provided at the top of the reactor housing, the product gas transport pipe being connected to the top of the gas collection chamber;
a gas outlet of the second solid-gas separator is connected to the gas collection chamber; a gas outlet of the first solid-gas separator is connected to the gas collection chamber;
The fluidized bed reactor further includes a spent agent circulation pipe provided outside the reactor housing,
2. The inlet of the spent agent circulation tube is connected to the spent agent region, and the outlet of the spent agent circulation tube is connected to the bottom of the reaction zone . Fluidized bed reactor. An apparatus, the apparatus comprising a fluidized bed reactor and a fluidized bed regenerator, the fluidized bed reactor communicating with the fluidized bed regenerator, and the fluidized bed reactor comprising: An apparatus characterized in that it is selected from the fluidized bed reactors described above. The fluidized bed regenerator includes a regenerator housing, the regenerator housing is provided with a spent catalyst inlet, and the spent catalyst inlet is in communication with a spent agent region of the fluidized bed reactor;
the spent catalyst inlet is in communication with a spent agent region of the fluidized bed reactor via a first stripper;
a bottom end of the regenerator housing is in communication with the coke control region;
a bottom end of the regenerator housing is in communication with the coke control region via a second stripper;
a regenerator heat remover is provided within the second stripper;
The regenerator housing further includes a regenerator distributor, one end of the second stripper extending into the regenerator housing;
The fluidized bed regenerator further includes a regenerator solid-gas separator, a regenerator gas collection chamber, and a flue gas transfer pipe, the regenerator solid-gas separator being disposed within the regenerator housing and A regenerator gas collection chamber and the flue gas transport pipe are provided at the top of the regenerator housing, the flue gas transport pipe is provided at the top end of the regenerator housing, and the flue gas transport pipe is located at the top of the regenerator housing. a gas outlet of the regenerator solid-gas separator is connected to the top of the gas collection chamber, a regenerated catalyst outlet of the regenerator solid-gas separator is connected to the bottom of the regenerator housing; 5. The device according to claim 4, characterized in that it is provided in a. A method for producing light olefins from oxygen-containing compounds, characterized in that the method is carried out using the fluidized bed reactor according to claim 1 . The method includes:
passing a coke control feedstock and a catalyst from a regenerator to a coke control region and reacting to produce a coke control catalyst and a coke control product gas;
the catalyst forming an annular flow through catalyst flow holes on a baffle plate ;
The method includes:
A coke control feed is passed from a coke control zone distributor into a coke control zone, a catalyst is passed through a catalyst inlet into a coke control zone, and the coke control feed and the catalyst are catalytically reacted in the coke control zone, and coke producing a control catalyst and a coke control product gas, the coke control catalyst entering the reaction zone via the coke control catalyst outlet, and the coke control product gas entering the transport pipe via the coke control gas outlet; 1) and
(2) feeding a feed containing oxygenates into a reaction zone from a reactant feed inlet and contacting a coke control catalyst to obtain a stream A containing light olefins;
The coke control raw material contains a C ₁ to C ₆ hydrocarbon compound,
The hydrocarbon compound is at least one selected from C ₁ to C ₆ alkanes and C ₁ to C ₆ alkenes,
The coke control raw material further includes at least one of hydrogen gas, an alcohol compound, and water, and the total mass content of the alcohol compound and water in the coke control raw material is 10 wt% or more and 50 wt%. The following is
The alcohol compound is at least one selected from methanol and ethanol,
The coke control raw materials include hydrogen gas 0-20 wt%, methane 0-50 wt%, ethane 0-50 wt%, ethylene 0-20 wt%, propane 0-50 wt%, propene 0-20 wt%, butane 0-90 wt%, butene. Contains 0-90 wt%, pentane 0-90 wt%, pentene 0-90 wt%, hexane 0-90 wt%, hexene 0-90 wt%, methanol 0-50 wt%, ethanol 0-50 wt%, water 0-50 wt%,
The hydrocarbon compound is not 0,
The process operating conditions in the coke control region are: gas apparent linear velocity of 0.1 to 0.5 m/s, reaction temperature of 300 to 700°C, reaction pressure of 100 to 500 kPa, and bed density of 400 to 800 kg/m3 ^. and
The process operating conditions in the reaction zone are : gas apparent linear velocity of 0.5 to 7.0 m/s, reaction temperature of 350 to 550°C, reaction pressure of 100 to 500 kPa, and bed density of 100 to 500 kg/m3 ^. 7. A method according to claim 6 , characterized in that. The oxygen-containing compound is at least one selected from methanol and dimethyl ether, the catalyst includes SAPO molecular sieve,
The coke content in the coke control catalyst is 4 to 9 wt,
the quartile deviation of the coke content distribution in the coke control catalyst is less than 1 wt%;
The coke species in the coke control catalyst include polymethylbenzene and polymethylnaphthalene,
The content of the total mass of the polymethylbenzene and polymethylnaphthalene in the total mass of coke is ≧70 wt%,
The content of the mass of coke species with a molecular weight >184 in the total mass of coke is ≦25 wt%;
Here, the total mass of coke is the total mass of coke species,
The method according to claim 7 , characterized in that the coke content in the spent catalyst is between 9 and 13 wt% . After the step (2),
forming a mixed stream B in a transport pipe of a stream A containing light olefins and a coke control product gas exiting from a coke control gas outlet, the flow B passing through the transport pipe to a first solid-gas separator; step (3) , which is separated into a gas phase stream C, which is a gas containing light olefins, and a solid phase stream D, which is a spent catalyst, after entering and being separated into solid and gas;
the gas phase stream C enters the gas collection chamber, the solid phase stream D enters the spent agent region, and passes the spent agent zone fluidizing gas into the spent agent zone from the spent agent zone fluidizing gas inlet; step (4) in which the spent agent zone fluidizing gas and its supported spent catalyst are brought into contact with the spent catalyst to form a stream E, the spent agent zone fluidizing gas containing nitrogen gas, water vapor, step (4) including at least one of the following;
Stream E enters the second solid-gas separator, and after being separated into solid-gas, it is divided into a gas-phase flow F, which is a spent agent zone fluidizing gas, and a solid-phase flow G, which is a spent catalyst. Stream F enters the gas collection chamber, solid phase flow G enters the spent agent region, gas phase stream C and gas phase stream F mix in the gas collection chamber to form a product gas, and the product gas Step (5) of entering the downstream process via the gas transport pipe;
the spent catalyst in the spent agent zone returns to the bottom of the reaction zone of the fluidized bed reactor via a spent agent circulation pipe (6);
The process operating conditions in the used agent area are: gas apparent linear velocity of 0.1 to 1.0 m/s, reaction temperature of 350 to 550°C, reaction pressure of 100 to 500 kPa, and bed density of 200 to 800 kg/m. 8. The method according to claim 7 , characterized in that: ³ . The method includes:
further comprising: spent catalyst in a spent agent zone enters the fluidized bed regenerator and enters the coke control zone after being regenerated in the fluidized bed regenerator;
The method includes:
step (a) of said spent catalyst entering the middle part of a fluidized bed regenerator after being stripped through a first stripper;
Regeneration gas is passed through the regeneration gas inlet to the bottom of the fluidized bed regenerator, contacting the regeneration gas with the spent catalyst and causing a chemical reaction to produce stream H containing flue gas and regenerated catalyst; enters the regenerator solid-gas separator, after solid-gas separation, it is divided into flue gas and regenerated catalyst, the flue gas enters the regenerator gas collection chamber, and then passes through the flue gas transport pipe to the downstream exhaust gas. After entering the smoke treatment system, the regenerated catalyst returns to the bottom of the fluidized bed regenerator, and the regenerated catalyst in the fluidized bed regenerator enters the second stripper, where it is stripped and heat removed before coke control of the fluidized bed reactor. (b) entering the region;
The regeneration gas is at least one selected from oxygen gas, nitrogen gas, water vapor, and air,
The regeneration gas contains 0 to 100 wt% air, 0 to 50 wt% oxygen gas, 0 to 50 wt% nitrogen gas, and 0 to 50 wt% water vapor,
The process operating conditions of the fluidized bed regenerator are: gas apparent linear velocity of 0.5 to 2.0 m/s, regeneration temperature of 600 to 750°C, regeneration pressure of 100 to 500 kPa, and bed density of 150 to 700 kg/m. ³ ,
10. A method according to claim 9 , characterized in that the coke content in the regenerated catalyst is ≦3 wt% .

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